Production of acetylene



Nov. 7, 1939. F .1. METZGER PRODUCTION ACETYLENE Filed July 18, 1936 2 sheets-sheet 1 ATTORNEYS Nov. 7, 1939.

F. J. METZGER PRODUCTION oF ACETYLENE Filed July 18, 1936 2 Sheets-Sheet 2 INVENTOR @M ATTORNEYS Patented Nov. 7, l1939 UNITED STATES PATENT oFFlcE PRODUCTION 0F AUETYLENE Application July 18, 1938, Serial No. 91,407

4Claims.

This invention relates to improvements in processes and apparatus for the production of acetylene from hydrocarbons, and more particularly from light or normally gaseous hydrocarbons, by a cracking or conversion operation in which the heat required for the cracking or conversion is obtained by the regulated localized intense combustion of a portion oi the hydrocarbons being cracked or converted.

The processes and apparatus of the invention are intended and adapted for the commercial production of acetylene from hydrocarbons in a continuous manner with the use of an apparatus oi simple construction and with the practice oi a process of economical operation such that the production can be continued for long periods o! time without objectionable interruption due to accumulation of carbon in the apparatus. In

A certain of its broader aspects the invention is applicable -to the production of acetylene from vaporized liquid hydrocarbons, as set forth in my companion application Serial No. 91,408. The invention will be more particularly set forth herein in connection with the production of acetylene from light or normally gaseous hydrocarbons.

According to the present invention a regulated localized intense combustion is accomplished, followed by a further combustion or reaction in a composite combustion zone, by the introduction, into a combustion and cracking chamber which is large in cross-section in relation to the jets, of a large number of individual and separate high velocity jets of hydrocarbon, and a large number of individual and separate high velocity jets of oxygen in such a way as to bring about simultaneous mixing of the high velocity jets and localized and intense combustion of part of the hydrocarbon at a large number of localized points or zones, followed by further composite combustion or reaction in a composite combustion or flame zone; and with this further composite reaction or combustion followed by cooling or quenching of the resulting gases and subsequent treatment of the resulting gases for the separation oi acetylene therefrom.

In the carrying out of the invention the amount of oxygen thus introduced locally in the form of high velocity jets at a large number of points is suiiicient to effect combustion of a part only oi the hydrocarbons, but the heat resulting from the combustion of the hydrocarbon with the oxygen is sufficient to produce cracking or conversion of substantial quantities of the hydrocarbons with the resulting production of substantial yields of acetylene in the resulting gases.

(Cl. 26o-679) While I do not wish to limit myself by any theoretical explanation ofthe precise reaction which takes place, yet I am led to believe that the separate and localized introduction of a large number of separate and individual high velocity jets of hydrocarbon gas and of oxygen results in localized intense combustion of a large ,number of individual localized zones where the jets oi.' oxygen come into contact with the jets of hydrocarbon and effect initial intense combustion in such localized zones, followed by further cornmingling of the individual jets into a composite zone where further combustion or reaction takes place and in which the reactions are completed such that the gases which escape and which are cooled or quenched are free or substantially so from free oxygen and contain substantial quantities of acetylene.

I have found it important to avoid admixture `oi' too much diluent with the oxygen which is introduced in the large number of oxygen jets for accomplishing the combustion of a part of the hydrocarbon gas. When steam is used, it should be admixed with. the hydrocarbon, and not with the oxygen. In such cases it is the large number of individual separate jets of admixed hydrocarbon vapors and steam andthe large number of separate individual jets of oxygen which are brought together to accomplish the localized combustion of a part of the hydrocarbon gas in a large number of localized individual zones merging into a flame zone to accomplish the completion of the conversion or cracking operation.

The introduction of the large number of separate individual jets of gaseous hydrocarbon and of oxygen, according to the present invention, is effected by directed jets such that eiective localized intense combustion is obtained followed by blending oi the gases in the composite flame zone which is continuously changing in the sense that the large number of individual high velocity jets and their combustion products are continually merging into the composite iiame zone and such that the products of the completed reactions are continuously removed and immediately cooled or quenched and subsequently treated for the recovery of acetylene therefrom.

In order to obtain the large number of directed jets of high velocity of both the hydrocarbon and the oxygen it is important to supply both the hydrocarbon and the oxygen to the individual jets under a sufiiciently high pressure to give directed jets of high velocity. When these directed jets are discharged into the large combustion and reaction chamber, the jets intermingle with each other locally, with expansion of the jets as they emerge at high velocity into the zone of lower pressure in the combustion and reaction chamber, and with decrease in velocity of the jets, and contact or intermingling of the jets locally followed by intermingling or mixing or blending in the large combustion chamber. Moreover, a large volume of hydrocarbon and oxygen is thus introduced with rapid and intense combustion in a relatively short time, usually a very small fraction of a second, and with a high velocity of the gases and vapors, and of the products of combustion and reaction, through the large chamber.

In carrying out `the process of the present invention oxygen of varying purity can be used, but it is used advantageously as oxygen of or higher, which is commercially available.

The invention includes the production of acetylene from various light or gaseous hydrocarbons. Gaseous hydrocarbons such as natural gas can thus be used and particularly natural gas with its normal content of higher hydrocarbons than methane which seem to be of importance in the production of substantial yields of acetylene, or with an increased content of higher hydrocarbons, which may be added to the natural gas. Normally gaseous hydrocarbons such as ethylene, ethane, propylene, propane, etc., or mixtures thereof can be employed with advantage.

The temperatures which are used in the reaction chamberaccording to the present process are considerably in excess of those used in ordinary cracking operations for the production of gasoline or pressure distillate, and considerably in excess of those used in the various cracking processes which have been proposed for the production of ethylene. While the temperatures attained at the zone where the localized combustion of the oxygen and hydrocarbon jets takes place are dimcult to measure, the temperatures of the Walls of the reaction chamber may be as high as 900 C. or 1020 C. or higher on the outside, with the temperature on the inside of the wall somewhat higher.

With some of the light or normally gaseous hydrocarbons, steam may be advantageously used in admixture with the hydrocarbon to modify the reaction or combustion somewhat, particularly with the higher gaseous hydrocarbons, such as propane, propylene, butane, etc. With methane, or natural gas, or hydrocarbon mixtures containing preponderating amounts of methane, the use of steam does not seem desirable. When steam is used with the higher gaseous hydrocarbons, it is admixed with the hydrocarbon, and not with the oxygen.

In carrying out the present process it is not necessary to preheat the hydrocarbon or oxygen fed to the reaction chamber, although it is advantageous to do so. The heat of combustion of the hydrocarbon is sufllcient to raise the temperature of the gases to a sufficient extent to accomplish the desired reaction, but the hydrocarbon may be preheated, e. g., to 300 C. with advantage. Where steam is used in admixture with such hydrocarbons as propane, the mixture should be preheated, e. g., above C. to prevent condensation of water. It is also desirable to preheat the oxygen, to increase the efficiency of the combustion.

For the production of about 100,000 cubic feet of gas per day containing up to 7 to 8% of acetylene a reaction chamber can be advantageously used consisting vof a carborundum tube about 4 inches in diameter and about 12 IlQhGS long. This cylinder may be provided at one end with a head of suitable metal having a large number of directed jets arranged in pairs, or as concentric jets, or otherwise. When the jets are arranged in pairs, one jet of each pair is used for hydrocarbon gases, and the other jet is used for the supply of oxygen. Instead of arranging the jets in pairs, a larger number of directed jets of oxygen may be used than of hydrocarbon, or vice versa, with proper direction of the jets to obtain the desired regulated localized mixing and combustion.

For an operation such as just referred to, and with a cylinder or reaction chamber about 4 inches in diameter, the head may thus be provided with 20 or 30 pairs of impinging or concentric jets; and for larger scale operation, using cylinders or reaction chambers l2 or 18 inches in diameter, the head may be provided with two or three hundred pairs of jets, although a much smaller or larger number of jets may be used, depending on the size of the apparatus, the size of the jets, etc. Instead of arranging the jets in pairs, there may be provided a plurality of jets for oxygen for each jet for hydrocarbon, or a plurality of jets for hydrocarbon for each jet for oxygen, as long as the arrangement is such as to give the intense localized combustion followed by a further combustion or reaction in a composite combustion or reaction zone.

At the other end of the cylinder, through which the exit gases iiow, there is advantageously provided a water spray which quenches and rapidly cools the exit gases and also aids in the removal of tar or carbon therefrom.

The apparatus is provided with suitable means for the regulation and control of the hydrocarbon and oxygen fedto the apparatus, and means for admixing the hydrocarbon gases with steam may be provided, if desired. There are also provided suitable scrubbers for the exit gases, to remove entrained tar and carbon therefrom, and suitable means for recovering the acetylene from the gases, or for converting the acetylene into other useful products, such as acetaldehyde.

The invention will be further illustrated by the accompanying drawings, and the process of the invention will be further described in connection therewith; but it will be understood that the invention is not limited thereto.

In the drawings:

Fig. 1 is a flow sheet or schematic representation of an apparatus suitable for the production of acetylene from propane, or similar hydrocarbons.

Fig, 2 illustrates in a somewhat conventional and diagrammatic manner a reaction chamber and head which may be used and which embodies the invention.

Fig. 3 shows conventionally and in somewhat greater detail the arrangement of one of the pairs of jets used in the head illustrated in Fig. 2.

Fig. 4 is a sectional view oi the head shown in Fig. 2; and

Fig. 5 is a somewhat conventional sectional view of a modified head which embodies the invention and which may be used with advantage.

In the apparatus conventionally shown in Fig. 1, which is adapted for the production of acetylene from such hydrocarbons as propane, the hydrocarbon is fed from the storage tank l, or other source of supply, in which it may be kept in liquid form under pressure, to a vaporizer 2, and thence through a reducing valve or valves 3, which regulate the pressure at which it is supplied 'to the apparatus. The hydrocarbon then passes to the pipe 4, from which, by proper Iinanipuiation of the valves I and 4 it may be fed directly to the reaction chamber 1 through pipes Ii and I2 or to the preheater l, consisting of 5 suitable pipes or coils in a furnace 3, whence it passes to the reaction chamber 'l through pipes Il and ill. If it is desired to admix steam with the hydrocarbon, this may be supplied through pipe I 3. controlled by valve I4, and the admixed steam land hydrocarbon may be passed through the preheater 3, or supplied directly to the reaction chamber 1.

The oxygen used in the process isv advanta` geously supplied from an oxygen plant I3, e. g., a liquefaction plant, in which it is produced from air as required. The oxygen is compressed in compressor I 3, and may be passed through line I1 and valve Il to heating coils I3 to be preheated, and then through pipes and 23 to the 2o reaction chamber, or through pipe 2l and valve 22, and pipe 23, directly to the reaction chamber 1, without preheating.

The construction of the reaction chamber 1, and the attached head and means for quench- 2li ing the exit gases from the chamber are illustrated, in a more or less conventional fashion,

in Figs. 2 to 5.

In Fig. 2, there is shown a suitable reaction tube 2B, which may be advantageously made of so carborundum or other refractory material, or

may be made of metal, with provision for causing a stream of water to iiow down its interior surface to protect the metal and keep it clean, surrounded by suitable insulation 23, inl casing 35 21. At the top of this tube is provided a head 28 into which is introduced the hydrocarbon `through pipe Il, and the oxygen separately through pipe 23. The hydrocarbon enters the upper chamber 23, while the oxygen enters the .w lower chamber 30, both provided within the head.

This head is advantageously made in three sections, a lower section 3i provided with holes for the nozzles, an upper section 32, and a middle section 33, which is provided with openings for the nozzles and which is formed with central recesses on both sides so that the chambers 23 and 30 are formed when the upper and lower plates are fastened to it.

'I'he head 23 is provided, as shown, with a m number of nozzles or jets through which the hydrocarbon and oxygen separately flow into the tube 25. The construction of these nozzles is illustrated in Fig. 3. Each nozzle includes a tube t4 which extends from the plate 33 through an M opening 33 in the plate 3|, forming a passageway from chamber 29 to the interior of the tube 25. The openings 33 in the plate 3l through which these tubes pass are somewhat larger than the outer diameter of the tubes 34 W as shown, so that there is an annular passageway around each of the tubes from the chamber 3U to the interior oi the tube 25.

The openings in the plate 3| are made somewhat smaller at the bottom of the plate than at @5 the top of the plate, and the tubes 34 are square in shape where they fit into the upper part of the openings, so that they are properly centered in the openings, while leaving suitable passageways for the flow of oxygen down past the tubes 34 im into the tube 25. This method of centering the tubes 34 is illustrated in Fig. 4, which shows how the square portions ofthe tubes 34 correctly center the tubes in the openings 36 while leaving spaces for the flow of the jets of oxygen. 75 The number of such nozzles, each of which f aivaave I 3 provides a ,iet of hydrocarbon through the central opening with an annular jet of oxygen'surrounding it, may vary; but in the apparatus i1- lustrated, with a tube about 4 inches by l2 inches and intended for the production of five to ten 5 thousand cubic feet of acetylene per day, about 19 such nozzles may be used, each, e. g.. with the diameter of the openings for the iiow of hydrocarbon about three-sixteenths of an inch, and with the area of the annular space through which 10 the oxygen flows about equal to that of the three-sixteenths inch opening.

Where the apparatus is intended for a larger scale operation, and the reaction chamber is made of a tube 12 to 18` inches in diameter, and 15 3 or 4 feet long, the number of nozzles may be increased about as the cross-sectional area of the tube, so that 200 or more such'nozzles may be provided; although with the larger scale ap-` paratus, the size of the nozzles may be some- 20 what increased, and their number may be less than the number which would be provided if the apparatus were simply enlarged to scale, so as to reduce the back pressure and the resistance to flow of the vapor and gases. The number may be as low as 50 or less, or as high as 300 or more, depending on the size ofthe apparatus, the size and shape of the nozzles, etc.

A modified arrangement of the head which may also be used with advantage is illustrated in Fig. 5. In this head, there is provided a plate 31, which has a number of obliquely cut holes 38, about one-eighth inch in diameter, arranged in concentric circles. These openings are arranged in pairs so that they produce directed jets of hydrocarbon and oxygen in pairs, the jets of each pair impinging as they come into the reaction tube. Above this plate is a box 33 with separate chambers into which the hydrocarbon is introduced through line Il, and the 40 oxygen through line 23. The hydrocarbon thus flows into the chambers 40 while the oxygen flows into the chambers 4i. The oxygen thus passes through the openings aaa, While the hydrocarbon ows through the openings bbb. With this head, when used with a combustion tube such as shown in Fig. 2, about 32 pairs of openings may be provided: and with a larger scale apparatus, thel number of openings provided may be increased in about the same ratio as the cross-sectional area of the reaction tube is increased.

Below the reaction tube 25 there is provided a metal tube 42 through which the exit gases flow. This tube is kept cool by a stream of water which flows down its inner surfaces, the water entering the annular chamber 43 from pipe 44 and owing over the upper portion of the tube 42 and down the inner surface oi the tube. This stream of water not only serves to keep the tube 42 cool, but also serves to prevent the deposition 60 oi carbon thereon.

The exit gases flow through this tube 42 into the chamber 45 where they are quenched and cooled by a water spray from nozzle 46. `The amount of water which is sprayed into the'gases G5 through nozzle 46 is greatly in excess of the amount of water which can be vaporized by the sensible heat of the gases, and is sufficient to cool the gases to a low temperature of e. g., about 40 C. more or less. The cooled gases. with ad- 70 mixed water, then pass through the pipe 41 to a suitable countercurrent washer 48. In this washer, which may be provided with baille plates 49, the gases and vapors are brought into contact with water introduced through pipe 50. '15,

This washer, together with the water spray, removes a large part of the tar and carbon from the gases. The water from the Washer, and the excess water sprayed into the gases by nozzle 46, flows into the water seal 5I and then into a settling basin 52 in which oil and tar are separated.

Instead of providing a water washer for the exit gases, the vapors and gases and Water from the nozzle 46 may be passed through a separator, in which the greater part of the water is removed, and then led to an oil scrubber. However, it is advantageous to provide a water scrubber, as the gases, even after the separation of entrained water from the nozzle 456, contain a good deal of Water vapor, and if they are cooled to any great degree in an oil scrubber or tar scrubber, tend to condense out water which forms an emulsion.

The gases and vapors, after having been scrubbed with water in the scrubber 38, are led by pipe 58 to a tar separator 5G. This separator, which may be of the bubble plate type, is shown of usual construction, and is provided with a tank 55 and a circulating pump 56 so that the scrubbing oil used may be circulated through the separator. In this separator, entrained tar and oil which the gases and vapors carry are removed. The vapors and gases then pass through a centrifugal separator 5l and through pipe 58 to the vessel 59, in which any hydrogen sulfide is removed by iron oxide. After the removal of any hydrogen sulde in this vessel, the gases and vapors pass to a suitable bubble plate column in which the light oils such as benzol are removed by scrubbing with a suitable absorbent, such as straw oil. From this tower, the gases and vapors, which now contain e. g., up to about 7 to 8% of acetylene, pass through pipe 6i to be treated for the recovery or use of the acetylene.

These purified gases, which contain e. g., from 7 to 8% of acetylene, may be treated directly for the production of acetaldehyde from the acetylene, or they may be passed into contact with a suitable solvent for acetylene for'the recovery of the acetylene in more concentrated form. For example, the gases may be brought into contact, as in a suitable scrubbing tower, with diethyl carbonate, which preferentially dissolves the acetylene, as described in my prior Patent No. 1,900,655. By bringing the gases while under pressure into contact wtih diethyl carbonate, and then boiling the acetylene off from the diethyl carbonate, the concentration of acetylene may be increased to as much as 60% or more, and by one or more repetitions of the treatment may be increased to above The concentrated acetylene-containing gases may be advantageously used for the production of acetaldehyde, or may be used in other ways or for other purposes.

It is o ne advantage of the process and apparatus of the present invention that high superatmospheric pressures are not required; nor does the process require the use of a vacuum. The invention can advantageously be practiced at pressures around atmospheric, or such that the gases emerge from the purifying apparatus at about atmospheric pressure. That is, the pressure in the various parts of the apparatus subsequent to the combustion or reaction chamber may be only sufiiciently above atmospheric to provide for the ow of the gases and vapors through these subsequent parts of the apparatus.

It is, however, important in those parts of the apparatus which precede the combustion or reaction chamber to have a sumcient pressure to insure introduction of the hydrocarbon and of the oxygen through the jets to give directed jets of both oxygen and hydrocarbon; and, where the exit gases from the purifying apparatus are at atmospheric pressure, it is also important that the pressure of the oxygen and hydrocarbon be also sufficient to insure flow of the gases through the apparatus from the reaction or combustion chamber to the purifier.

The pressure drop through the jets and the pressure required to force the oxygen and hydrocarbon through the jets with suicient velocity will vary somewhat with the size and construction of the jets and may be e. g., 3 pounds per square inch. The pressure drop throughout the subsequent parts of the apparatus will vary with the construction and arrangement of the apparatus but may be, for example, around 2 or 3 pounds or more per square inch. The necessary pressure of the oxygen and of the hydrocarbon is readily obtained by supplying the same under the necessary pressure to the respective large numbers of jets.

When thel apparatus is used for the production of acetylene from natural gas, methane, mixtures of methane and higher hydrocarbons, ethylene, ethane, etc., available in a gaseous state, i. e., unliqueiied, the vaporizer is unnecessary, and the hydrocarbon may be supplied directly to the reaction chamber, but even with such gaseous hydrocarbons, it is advantageous to preheat them as the efficiency of the operation is somewhat increased if the gases are preheated.

Acetylene can be produced in substantial amounts from natural gas by the process of the present invention, particularly where the natural gas has a substantial content of hydrocar bons heavier than methane, such as ethane, propane, etc., or where such higher hydrocarbons have been added to a natural gas poor in them, or to methane. Apparently the content of such higher hydrocarbons in the natural gas has an important effect on the amount of acetylene produced. Such hydrocarbons as ethane, ethylene, propane, propylene, butane, etc., and mixtures thereof, or mixtures containing substantial amounts of these hydrocarbons, all yield substantial amounts of acetylene when treated in accordance with this invention.

The invention will be further illustrated by the following specilc examples, but it is not limited thereto.

Eample I.-For the production of acetylene from propane, using the apparatus of Fig. 2 with a reaction tube 4 inches by l2 inches, and concentric nozzles, about 970 cubic feet of propane, measured at atmospheric temperature and pressure, suitably preheated to about 210 C, and about 1130 cubic feet of oxygen, measured at atmospheric temperature and pressure, and preheated to about 250 C. are introduced per hour into the reaction chamber. Under such cond1 tions, the outside Wall of the reaction tube may have a temperature of from 820 C. to abou!l 900 C. The exit gases, after prompt quenching, purification and removal of water, had, in one instance, the following composition:

'When operated in this manner, the apparatus produces about 250 cubic feet of acetylene per hour. By increasing the velocity of fiow of the gases, and ,increasing the input to the apparatus, theproduction of acetylene can be increased, as much as 8,000 cubic feet of acetylene per day being obtainable from propane with the use of such a reaction tube as above described. 0perating in this manner. about 100,000 cubic feet 1o of gas which may contain up to about 8% oi acetylene can be produced per day.

Example .IL- About i130 cubic feet of oxygen and 9.45 cubic feet of propane, measured at atmospheric temperature and pressure. are intro-l` duced into a 4 inch carborundum reaction tube, provided with a head such as illustrated in Fig. 5, per hour, without preheating. In one case, about 3520 cubic feet of dry exit gas were obtained per hour, containing about 7.3% of acetylene.

Example IIL-About 1060 cubic reet of oxygen, preheated to about 320 C., and about 954 cubic feet of propane, admixed with about 25 pounds of steam, the mixture being heated to about 292 C., are introduced per hour into a reaction chamber 25 similar to that used in Example II. In one instance, an exit gas containing about 7.8% of acetylene was obtained.

lt'cmplc IV.-In another run, underthe same conditions as in Example III, except that about :lo 5l pounds of steam per hour was admixed with the propane, an exit gas containing about 7.7% oi? acetylene was obtained.

Example V.About 1060 cubic feet of oxygen, preheated to about 453 C., and about 974 cubic feet of propane, preheated to about 397 C., are supplied per hour to a reaction chamber similar to that of Example II. In one case, an exit gas containing about 8.4% of acetylene was obtained.

Example VI.A natural gas containing about 83.1% methane, 11.2% ethane, 3.4% propane, 0.8% butano and 1.5% nitrogen was supplied to a reaction chamber similar to that of Example II at the rate of about 1730 cubic feet per hour, along with about 1360 cubic feet of oxygen per hour. In

L was obtained, having the following composition:

Percent C2H2 5.1 Co2 4.0 U can 0.5 O2 0.0 CO 25.2 Cllr-Hilft (by diff.) 65.2

It will thus be seen that by the present invention l provide a new and improved process by which acetylene may be produced from more saturated light or gaseous hydrocarbons, which may be obtained from various sources, and which may vary Widely in character, in large quantities and with apparatus which can be run for long periods of time without dismantling for cleaning or other purposes. When cleaning is required, the head can be readily removed and replaced.

The acetylene produced by the present process may be used for chemical manufacture or for other purposes, and the other gases which are produced as by-products can be advantageously used for fuel or for the manufacture of such products as synthetic alcohols.

It will further be seen that the process of the invention involves the separate introduction of a large number of directed jets of oxygen or a gas rich in oxygen, and a large number of jets of hydrocarbon into a reaction or combustion chamone instance, about i900 cubic feet of dry exit gasl ing and burned products in a composite ame or reaction zone to permit the completion of the reaction.

The apparatus oi' the present invention includes the new and improved combustion or reaction chambers and a new and improved head for the' supply of a large number of directed and separate high velocity jets of oxygen and hydrocarbon, so arranged that each directed high velocity jet of oxygen impinges upon or is surrounded or comes into intimate contact with, one or more directed" high velocity jets of hydrocarbon vapor, or so that each directed high velocity jet oi' hydrocarbon impinges upon, or is surrounded by. or comes into intimate contact with one or more high ve locity jets or oxygen, in combination with a suitable reaction chamber, comprising an open, unrestricted tube advantageously made of carborundum or other suitable refractory material; and in combination with means for supplying the hydrocarbons and oxygen to the jets under a sufficiently high pressure, and means for quickly removing and cooling theresulting gases. I do not in this application claim the apparatus herein described, as it is claimed in my divisional application Serial No. 252,639, filed January 24, 1939.

In its broader aspects, as previously pointed out, certain features of the present invention are applicable to the productionloi acetylene from vaporized liquid hydrocarbons; particularly when such hydrocarbon vapors are admixed with steam before introducing them as separate individual Jets into the composite composition and reaction chamber, as set forth more particularly in my companion application Serial No. 91,408, in 'which the production of acetylene from such normally liquid hydrocarbons is claimed. The broader aspects of the invention, applicable to both vaporizedV liquid and normally gaseous hydrocarbons, is claimed herein, with specic claims directed to the process in which the normally gaseous hydrocarbons are employed.

I claim:

l.. In the process oi producing acetylene from more saturated hydrocarbons by combustion with an amount of oxygen insumcient for complete combustion, the improvement which comprises introducing into a large combustion and reaction chamber a large number oi separate high velocity jets of gaseous hydrocarbon and a large number of separate high velocity jets of oxygen, the jets being so directed as to cause commingling and combustion in a localized and regulated manner and with blending of the resulting jets and products ci combustion in a composite combustion or reaction Zone.

2. In the process of producing acetylene from more saturated hydrocarbons by combustion with an amount of oxygen insuiilcient for complete combustion, the improvement whichl comprises `supplying the hydrocarbon in a gaseous or vaporous form under pressure, separately supplying oxygen under pressure, causing the hydrocarbons and oxygen to discharge separately through a. large number of directed jets at high velocity into a large combustion and reaction chamber, with resulting expansion and reduction in velocity of the individual jets and localized combustion followed by further blending or mingling of the jets and products of combustion in a composite combustion or reaction zone.

3. In the process of producing acetylene from more saturated hydrocarbons by combustion with an amount of oxygen insufficient for complete combustion, the improvement which comprises introducing, into a relatively large combustion chamber, a large number of separate individual jets of hydrocarbon and oxygen at a high velocity, said jets being arranged in pairs so that the jets of hydrocarbon impinge upon, or come into intimate contact with, the jets of oxygen, causing combustion of the gases thus introduced and combining of the same in a composite combustion or reaction zone.

4. In the process of producing acetylene from more saturated hydrocarbons by combustion with an amount of oxygen insufficient for complete combustion, the improvement which comprises introducing, into a relatively large combustion or reaction chamber, and in a continuous manner, a large number of individual directed jets of hydrocarbon in gaseous or vapor form at high velocity, separately introducing a large and corresponding number of individual directed jets of oxygen at high velocity, directing the respective jets to cause localized initial combustion in a large number of localized combustion zones, followed by blending or intermingling of the products of initial combustion in a further composite combustion zone, causing the gases to pass through the combustion or reaction chamber at high velocity and promptly cooling the resulting gases.

FLOYD J. METZGER. 

